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EP2308592A1 - Abgasreinigungskatalysator und abgasreinigungsverfahren - Google Patents

Abgasreinigungskatalysator und abgasreinigungsverfahren Download PDF

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Publication number
EP2308592A1
EP2308592A1 EP09800263A EP09800263A EP2308592A1 EP 2308592 A1 EP2308592 A1 EP 2308592A1 EP 09800263 A EP09800263 A EP 09800263A EP 09800263 A EP09800263 A EP 09800263A EP 2308592 A1 EP2308592 A1 EP 2308592A1
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Prior art keywords
catalyst
component
exhaust gas
honeycomb structure
oxide
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EP09800263A
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English (en)
French (fr)
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EP2308592B1 (de
EP2308592A4 (de
Inventor
Katsuaki Kato
Yoshiro Hirasawa
Takashi Yamada
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NE Chemcat Corp
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NE Chemcat Corp
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/19—Catalysts containing parts with different compositions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
    • B01D53/94—Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
    • B01D53/9445—Simultaneously removing carbon monoxide, hydrocarbons or nitrogen oxides making use of three-way catalysts [TWC] or four-way-catalysts [FWC]
    • B01D53/945—Simultaneously removing carbon monoxide, hydrocarbons or nitrogen oxides making use of three-way catalysts [TWC] or four-way-catalysts [FWC] characterised by a specific catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
    • B01D53/94—Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
    • B01D53/9459—Removing one or more of nitrogen oxides, carbon monoxide, or hydrocarbons by multiple successive catalytic functions; systems with more than one different function, e.g. zone coated catalysts
    • B01D53/9477—Removing one or more of nitrogen oxides, carbon monoxide, or hydrocarbons by multiple successive catalytic functions; systems with more than one different function, e.g. zone coated catalysts with catalysts positioned on separate bricks, e.g. exhaust systems
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B01J23/58—Platinum group metals with alkali- or alkaline earth metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B01J23/63—Platinum group metals with rare earths or actinides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/024—Multiple impregnation or coating
    • B01J37/0244—Coatings comprising several layers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/024—Multiple impregnation or coating
    • B01J37/0248—Coatings comprising impregnated particles
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N3/00—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust
    • F01N3/08—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous
    • F01N3/10—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous by thermal or catalytic conversion of noxious components of exhaust
    • F01N3/24—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous by thermal or catalytic conversion of noxious components of exhaust characterised by constructional aspects of converting apparatus
    • F01N3/28—Construction of catalytic reactors
    • F01N3/2803—Construction of catalytic reactors characterised by structure, by material or by manufacturing of catalyst support
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/10—Noble metals or compounds thereof
    • B01D2255/102—Platinum group metals
    • B01D2255/1021—Platinum
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D2255/00—Catalysts
    • B01D2255/10—Noble metals or compounds thereof
    • B01D2255/102—Platinum group metals
    • B01D2255/1023—Palladium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/10—Noble metals or compounds thereof
    • B01D2255/102—Platinum group metals
    • B01D2255/1025—Rhodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/204—Alkaline earth metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
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    • B01D2255/20—Metals or compounds thereof
    • B01D2255/206—Rare earth metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/207—Transition metals
    • B01D2255/20715—Zirconium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/90—Physical characteristics of catalysts
    • B01D2255/902—Multilayered catalyst
    • B01D2255/9022—Two layers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
    • B01J21/04—Alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/066—Zirconium or hafnium; Oxides or hydroxides thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J23/44—Palladium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J23/46—Ruthenium, rhodium, osmium or iridium
    • B01J23/464—Rhodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • B01J37/0027—Powdering
    • B01J37/0036—Grinding
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N2510/00—Surface coverings
    • F01N2510/06—Surface coverings for exhaust purification, e.g. catalytic reaction
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
    • Y02T10/00—Road transport of goods or passengers
    • Y02T10/10—Internal combustion engine [ICE] based vehicles
    • Y02T10/12—Improving ICE efficiencies

Definitions

  • the present invention relates to an apparatus of a catalyst for purifying exhaust gas exhausted from an automobile and a method for purifying exhaust gas using this catalyst apparatus, and in particular, relates to an apparatus of a catalyst for purifying exhaust gas suitable as a three-way catalyst (TWC) apparatus to be used for purifying carbon monoxide (CO), a hydrocarbon (HC) and a nitrogen oxide (NO x ) in exhaust gas exhausted from a gasoline automobile and a method for purifying exhaust gas.
  • TWC three-way catalyst
  • platinum (Pt), palladium (Pd) and rhodium (Rh) are known, which have been used widely as the catalyst for purifying exhaust gas exhausted from an internal combustion engine of an automobile or the like.
  • catalytically active species superior in oxidation activity such as Pt and Pd
  • Rh superior in purification activity of NO x are used in combination in many cases.
  • strictness of regulations for harmful substances, in particular, NO x contained in exhaust gas has been increasing. Therefore, it is necessary to use efficiently Rh superior in purification activity of NO x .
  • output of Rh is low, Rh is expensive and market price thereof has been rising in recent years. Therefore, it is preferable to reduce use amount of Rh as catalytically active species, in view of resource protection or a cost aspect.
  • an oxygen storage component (OSC), an alkaline earth metal, zirconium oxide, zeolite or the like.
  • OSC oxygen storage component
  • cerium oxide stores oxygen as CeO 2 , when oxygen concentration in exhaust gas is high, and discharges oxygen by being converted to Ce 2 O 3 , when oxygen concentration is low.
  • Oxygen discharged is active oxygen and promotes purification of HC or CO by being utilized in oxidation action by Pt or Pd.
  • the OSC also acts to buffer the oxygen concentration change in exhaust gas.
  • purification performance of exhaust gas enhances.
  • the TWC performs oxidation and reduction by one catalyst, and has a range of exhaust gas components suitable for purification in view of designing. This range depends on air / fuel ratio in many cases. Such a range is referred to as a window, and in many cases, exhaust gas combusted at the vicinity of theoretical air / fuel ratio is set as the window region.
  • this window region can be maintained for a long period, and purification of exhaust gas is performed efficiently. It has been said that this has influence, in particular, on purification performance of NO x by RH.
  • cerium oxide pure cerium oxide may also be used, however, it is used as a composite oxide with zirconium (refer to Patent Document 2) .
  • the cerium-zirconium composite oxide has high heat resistance, and is said to have high storing and discharging rate of oxygen.
  • Reason for this is considered that a crystal structure of the cerium-zirconium composite oxide is stable, by which an action of a cerium oxide, which is a major OSC component, is not obstructed, and can be utilized in an action as the OSC up to the inside of particles.
  • the alkaline earth metal such as a Ba component
  • the Ba component temporarily stores NO x contained in exhaust gas, and purifies NO x stored by reducing to N 2 by a reducing component contained in exhaust gas.
  • NO x generates in a large quantity, when fuel supplied to an engine is less and amount of air is much.
  • the Ba component temporary absorbs NO x generating in this way.
  • NO x absorbed by the Ba component is discharged from the Ba component when concentration of NO x in exhaust gas is low, and CO concentration becomes high.
  • this is derived from a reaction of the Ba(NO 3 ) 2 with CO to become BaCO 3 and may be said chemical equilibrium.
  • NO x discharged from the Ba component as described above, reacts with reducing components at the surface of the Rh component to be reductively purified.
  • Such a co-catalyst component may be used in combination of two or more kinds, for example, the TWC using the Ba component and cerium oxide has been known (refer to Patent Document 5).
  • purification performance may be decreased depending on a combination of catalyst materials, for example, presence of the Rh component and the Ba component in the same composition is reported to decrease purification performance of NO x (refer to Patent Document 6) .
  • Reason for this is not certain, however, because the alkaline earth metal component has an action of storing NO x , it is considered that purification performance of NO x in the Rh component is obstructed, or the Ba component and the Rh component may produce an alloy. In this way, there are various combinations of catalyst components, and because of passing a complicated reaction route by mutual interaction of the catalyst components, combinations of the catalyst components exerting purification performance most have been searched by comprehensive study thereof.
  • the catalyst for purifying exhaust gas may be enough to be arranged at one place in a flow passage of exhaust gas, however, there may be the case where two or more are arranged. Because in this way, surface area of the catalyst is increased, purification performance of exhaust gas is enhanced.
  • the catalyst for purifying exhaust gas such as the TWC has a window region in view of designing, simple arrangement of a plurality of catalysts may not provide desired catalyst for purifying exhaust gas in some cases. It is because components of exhaust gas passed through the catalyst at the front stage are different from those of exhaust gas just after being exhausted from an engine, it is necessary to design composition of exhaust gas thus changed as the window region.
  • the present applicant has also proposed a catalyst system, where two catalysts having a platinum group metal and an oxygen storage component (OSC) as the catalyst components are arranged in a exhaust gas flow passage (refer to Patent Document 7) .
  • OSC oxygen storage component
  • an object of the present invention to provide an apparatus of a catalyst for purifying exhaust gas and a method for purifying exhaust gas for purification by contacting , harmful substances contained in exhaust gas exhausted from an internal combustion engine of an automobile or the like, with the catalyst, and in particular, to provide an apparatus of a catalyst for purifying exhaust gas and a method for purifying exhaust gas superior in purification performance of NO x as an apparatus of catalyst for purifying exhaust gas using the TWC catalyst.
  • the present inventors have intensively studied a way to solve the above-described conventional problems and found that a hydrocarbon (HC), carbon monoxide (CO) and a nitrogen oxide (NO x ) can be purified efficiently by configuring an apparatus of a catalyst for purifying exhaust gas for purifying a hydrocarbon (HC), carbon monoxide (CO) and a nitrogen oxide (NO x ), by providing two or more honeycomb structure-type catalysts, wherein the surface of a honeycomb-type structure is coated with two or more layers of catalyst compositions, in a flow passage of exhaust gas exhausted from an internal combustion engine, and making exhaust gas pass; and by setting so that the honeycomb structure-type catalyst positioned at the upstream side and the honeycomb structure-type catalyst positioned at the downstream side, contain a support material of an inorganic oxide which substantially does not contain an Rh component, and loads at least one of a Pt component and a Pd component, a cerium-containing oxide, and an alkaline earth metal component, in all of the lower layers; on the other hand,
  • the catalyst (X) contains the support material of the zirconium oxide as a main component which load a Rh component on the support material of zirconium oxide and substantially does not contain a cerium component, and a cerium-containing oxide which substantially does not load the Rh component, and the catalyst (X) does not substantially contain Pt component and Pd component.
  • the catalyst (Y) contains the support material of the cerium-zirconium composite oxide as a main component which load a Rh component on the support material of cerium-zirconium composite oxide and which contains cerium of 1 to 20% by weight, in an oxide equivalent, and zirconium of 99 to 80% by weight, in an oxide equivalent, and the catalyst (Y) does not substantially contain Pt component and Pd component.
  • the apparatus of a catalyst for purifying exhaust gas characterized in that the support material of the inorganic oxide contained in the lower layer of the honeycomb structure-type catalyst (X) and the honeycomb structure-type catalyst (Y) is alumina.
  • the apparatus of a catalyst for purifying exhaust gas characterized in that the alkaline earth metal component contained in the lower layer of the honeycomb structure-type catalyst (X) and the honeycomb structure-type catalyst (Y) is a barium component.
  • the apparatus of a catalyst for purifying exhaust gas characterized in that the cerium-containing oxide contained in the lower layer of the honeycomb structure-type catalyst (X) and the honeycomb structure-type catalyst (Y) is the cerium-zirconium composite oxide.
  • the apparatus of a catalyst for purifying exhaust gas characterized in that amounts of the lower layer catalyst components of the honeycomb structure-type catalyst (X) and the honeycomb structure-type catalyst (Y) are as follows, per unit volume:
  • the apparatus of a catalyst for purifying exhaust gas characterized in that amounts of the upper layer catalyst components of the honeycomb structure-type catalyst (X) are as follows, per unit volume:
  • the apparatus of a catalyst for purifying exhaust gas characterized in that amounts of the upper layer catalyst components of the honeycomb structure-type catalyst (Y) are as follows, per unit volume:
  • the apparatus of a catalyst for purifying exhaust gas characterized in that the honeycomb-type structure is a flow-through-type honeycomb-type structure having a cell density of 10 to 1500 cell/inch 2 .
  • a purification method for exhaust gas characterized in that a hydrocarbon (HC), carbon monoxide (CO) and a nitrogen oxide (NO x ) are purified by supplying exhaust gas from an internal combustion engine to the apparatus of a catalyst for purifying exhaust gas, and by making it sequentially contacted with the honeycomb structure-type catalyst (X) at the upstream side of the exhaust gas flow passage and the honeycomb structure-type catalyst (Y) at the downstream side of the exhaust gas flow passage.
  • HC hydrocarbon
  • CO carbon monoxide
  • NO x nitrogen oxide
  • the purification method for exhaust gas characterized in that the internal combustion engine is a gasoline engine, and gasoline fuel is combusted under control to lean-rich states from theoretical air / fuel ratio.
  • the present invention by using two or more honeycomb structure-type catalysts having each different catalyst composition; arranging them at the upstream side and the downstream side in a exhaust gas flow passage; setting that the lower layer of the honeycomb structure-type catalyst contains a support material of an inorganic oxide which substantially does not contain an Rh component, and loads at least one of a Pt component and a Pd component, a cerium-containing oxide, and an alkaline earth metal component; on the other hand, in the upper layer, by setting that kind of a support material of an inorganic oxide loading the Rh component is changed for the upstream side catalyst and the downstream side catalyst, and substantially the Pt component and the Pd component are not contained; an apparatus of a catalyst for purifying exhaust gas can be provided, which exerts superior capability in purification of NO x in exhaust gas, generating in a large amount when an engine using fossil fuel is operated, in particular, in a lean-burn state.
  • HC or CO can be purified following variation of concentration or temperature of exhaust gas at the position where the honeycomb structure-type catalyst is provided, as well as high purification performance of NO x can be obtained.
  • the apparatus of the catalyst for purifying exhaust gas of the present invention is one, as shown in Figure 1 , for arranging each one or more honeycomb structure-type catalysts, having at least specific layer configuration, at the upstream side (2) and the downstream side (3) of a catalyst container (1) provided in a flow passage of exhaust gas exhausted from an internal combustion engine, and is one for purifying harmful components, by making exhaust gas pass through this.
  • honeycomb structure-type catalysts are used in the apparatus of the catalyst for purifying exhaust gas of the present invention.
  • the surface of a honeycomb-type structure is coated with two or more layers of catalyst compositions with different composition. It is because of avoiding offset of each catalytic activity by a composition for promoting oxidation of HC or CO, and a composition for promoting reduction of NO x , and not using, in the same layer, materials which result in decreasing activity caused by sintering or the like when positioned adjacently, so as to still more enhance purification efficiency of exhaust gas by utilizing also synergy effect of each layer.
  • the catalyst composition When the catalyst composition is arranged in multiple layers, in the catalyst layer at the upper side which tends to contact with exhaust gas components, purification of the exhaust gas components tends to be promoted more as compared with the catalyst layer at the lower side. Therefore, catalytically active species of the upper layer may exert high purification activity even in small amount.
  • a catalyst layer arranged in the upper layer is referred to as the upper layer catalyst layer (or, simply, the upper layer)
  • a catalyst layer arranged at the lower side of the upper layer is referred to as the lower layer catalyst layer (or, simply, the lower layer).
  • both of the honeycomb structure-type catalyst (X), which is the upstream side catalyst, and the honeycomb structure-type catalyst (Y), which is the downstream side catalyst have the same catalyst composition in the lower layer, and at least either of the Pt component or the Pd component, the cerium-containing oxide (not shown), and the alkaline earth metal component (indicated as "alkali-earth" in the drawing) are contained.
  • ZrO 2 loading the Rh component, and a cerium-containing oxide not loading the Rh component are contained in the upper layer of the upstream catalyst.
  • the cerium-containing oxide in the upper layer of this upstream catalyst is indicated as the OSC in the drawing.
  • the Rh component loaded on CeO 2 ⁇ ZrO 2 is contained in the upper layer of the downstream catalyst.
  • the cerium component in CeO 2 ⁇ ZrC 2 is indicated as "Ceria" in the drawing.
  • the cerium component in CeO 2 ⁇ ZrO 2 changes to CeO 2 and Ce 2 O 3 by oxidation and reduction accompanying with storage and discharge of oxygen.
  • the lower layer which is a carrier side of the honeycomb structure-type catalyst to be used in the present invention, at least one of the Pt component and the Pd component loaded on a heat resistant inorganic oxide is contained.
  • the Pt component and the Pd component are catalytically active species exerting oxidation activity.
  • the Pd component is cheaper than the Rh component and the Pt component, and even by using in a relatively large amount, a catalyst can be designed at a price easily acceptable on the market. Therefore, it is preferable that the Pd component is used in the lower layer, as all of or a major component of a noble metal component.
  • the Pd component tends to decrease catalytic activity caused by poisoning by a sulfur component. Therefore it is desirable that a large amount of the Pd component is used, or it is used in exhaust gas exhausted by using fuel containing low amount of the sulfur component.
  • a catalyst using the Pd component as all of or a major component of the noble metal component is the TWC to be used for purification of exhaust gas exhausted from a gasoline engine.
  • the lower layer of the honeycomb structure-type catalyst used in the present invention substantially does not contain the Rh component.
  • a catalytically active specie exerting oxidation activity such as the Pt component and the Pd component, and the Rh component exerting reduction activity are present in the same layer, each activity may be offset in some cases.
  • Pd is also a metal having fear of alloying or sintering with Rh, and both metals sintered may decrease activity in some cases ( JP-A-2002-326033 , paragraph 0004). Therefore, it is desirable to avoid presence of the Pd component and the Rh component in the same catalyst layer.
  • Basic composition in this lower layer is similar both in the honeycomb structure-type catalyst (X) at the upstream side, and the honeycomb structure-type catalyst (Y) at the downstream side.
  • the honeycomb structure-type catalyst to be used in the present invention is made in multiply layers, and in the lower layer, at least either of the Pt component and the Pd component loaded on the support material of the inorganic oxide, the cerium-containing oxide which substantially does not load the Pt component and the Pd component, and the alkaline earth metal component are contained.
  • the Pt component or the Pd component is contained in each catalyst composition in an amount of 0.01 to 10 g/L, desirably 0.05 to 9 g/L.
  • the too much amount increases concentrations of the Pt component and the Pd component, by which sintering may proceed excessively in some times in exposure to high temperature in use. When sintering proceeds, surface area of the Pt component and the Pd component decreases and activity decreases. In addition, the too less amount does not provide sufficient activity necessary, due to absolute lack of number of an active site.
  • the Pt component and the Pd component both have oxidation activity of CO or HC, however, the pt component is expensive although having high oxidation activity, while the Pd component is cheaper as compared with the Pt component. Therefore, us of the Pd component enables to reduce use amount of the Pt component.
  • the support material loading the Pt component and the Pd component is not especially limited, as long as it is porous, has heat resistance and is capable of maintaining high specific surface area value even in exhaust gas, and it may be selected from alumina, zirconia, titania, silica, silica-alumina, zeolite or the like, which are used in a catalyst for automotive exhaust gas.
  • a support material having high heat resistance and high specific surface area is capable of maintaining a highly dispersed state of the Pt component and the Pd component, and exerting superior purification performance, even in high temperature exhaust gas.
  • a heat resistant inorganic oxide alumina is preferable and among them ⁇ -alumina is preferable.
  • ⁇ -alumina has high heat resistance and high specific surface area, and is superior in dispersing property of the Pt component and the Pd component. And, in the case of ⁇ -alumina, it is preferable that lanthanum is added still more. ⁇ -alumina added with lanthanum is superior in heat resistance, and has been known that when a noble metal component is loaded, it maintains high catalytic activity even at high temperature ( JP-A-2004-290827 ). Specific surface area value (measured by a BET method; the same hereafter) of such ⁇ -alumina or ⁇ -alumina added with lanthanum is preferably 80 to 250 m 2 /g, and still more 200 to 250 m 2 /g is more preferable.
  • the specific surface area of ⁇ -alumina is equal to or lower than 250 m 2 /g, a catalyst with high heat resistance can be obtained.
  • the specific surface area of equal to or higher than 80 m 2 /g can stabilize a noble metal component in a highly dispersed state.
  • Alumina is contained in each catalyst composition, in an amount of 1 to 300 g/L, and more desirably 15 to 200 g/L.
  • the too much amount increases thickness of the catalyst layer excessively and makes difficult to raise catalyst temperature up to temperature suitable for purification. In addition, thus thickened catalyst layer obstructs gas diffusion to a deep part of the catalyst layer, resulting in not providing sufficient activity.
  • the too less amount increases concentration of the Pt component or the Pd component in the catalyst composition, resulting in proceeding of sintering of the Pt component or the Pd component, in exposure to high temperature in use, and not providing activity comparable to the use amount.
  • this alumina is used as a support material loading the above Pt component and the Pd component, however, it can be used not only as such a support material loading the Pt component and the Pd component, but also as a binder, by adding to the catalyst composition.
  • the alkaline earth metal component is contained in both of the upstream catalyst and the downstream catalyst, in the lower layer thereof.
  • the alkaline earth metal component is made contained in the lower layer, because presence thereof in the same layer with the Rh component in the upper layer decreases purification performance of NO x ( JP-A-2002-326033 , [0013]).
  • the reason for this effect is not certain, however, it is considered to be brought about by the facts that the alkaline earth metal component has an action of storing NO x , thus obstructing a purification action of NO x in the Rh component, and the Ba component and the Rh component produce an alloy.
  • the Rh component should be used in the upper layer aiming at promoting purification performance of NO x , therefore the alkaline earth metal component is used in the lower layer.
  • the Ba component having storing capability of NO x for example, barium oxide
  • the Ba component having storing capability of NO x can be used. It may be added into the catalyst composition as barium oxide, however, as a raw material of the barium component, one selected as appropriate from barium acetate, barium sulfate, barium carbonate, barium nitrate, barium sulfite or the like may be used.
  • the raw material of the NO x storing component other than barium oxide is fired in the production step of the honeycomb structure-type catalyst, and finally converted to barium oxide, or a composite material of barium oxide and other barium components.
  • Barium oxide contained in the catalyst stores NO x by generating barium nitrate, Ba(NO 3 ) 2 , by reacting with NO x .
  • NO x stored as Ba(NO 3 ) 2 is reductively purified to N 2 by a reaction with CO or HC etc., by reversed spill over, when a reducing component such as CO or HC is increased in exhaust gas.
  • CO or HC etc. is also oxidation purified ( JP No. 3488487 , paragraphs 0005 and 0013).
  • the alkaline earth metal component is contained in the catalyst composition in an amount of 0. 05 to 30 g/L, and desirably 1 to 20 g/L, in an oxide equivalent.
  • the too much amount progresses sintering of the alkaline earth metal, and may not provide effect corresponding to the addition amount. On the contrary, the too less amount may not provide sufficient addition effect of the alkaline earth metal in some cases.
  • cerium-containing oxide in which the Rh component is not loaded, may be contained.
  • the cerium-containing oxide is contained in the catalyst composition in an amount of 0.5 to 200 g/L, and desirably 1 to 100 g/L.
  • the too much amount increases thickness of the catalyst layer excessively and makes difficult to raise catalyst temperature up to temperature suitable for purification. On the contrary, the too less amount cannot absorb variation of oxygen concentration in exhaust gas sufficiently, and may deteriorate purification performance of NO x .
  • CeO 2 / ZrO 2 (B) CeO 2 / ZrO 2
  • CeO 2 / ZrO 2 (B) is not especially limited, however, it preferably has a cerium content of 10 to 70% by weight, and more preferably 30 to 60% by weight, in an oxide equivalent.
  • the too much amount of the cerium component results in sintering at high temperature and may decrease capability as the OSC. In addition, the too less amount may not exert sufficient capability as the OSC.
  • the catalyst composition is coated onto the honeycomb-type structure layer-likely.
  • the honeycomb-type structure as such a carrier is a flow-through-type honeycomb-type structure having a cell density of 10 to 1500 cell / inch 2 , and in particular, a flow-through-type carrier having a cell density of 300 to 900 cell / inch 2 .
  • the cell density of equal to or higher than 10 cell / inch 2 is capable of securing contact area between exhaust gas and a catalyst required in purification, and providing purification performance of exhaust gas with superior structural strength as well, while the cell density of equal to or lower than 1500 cell / inch 2 is capable of sufficiently securing contact area between exhaust gas and the catalyst without largely losing pressure of exhaust gas of an internal combustion engine, and without impairing performance of the internal combustion engine.
  • the flow-through-type carrier having a cell density of 300 to 900 cell / inch 2 is preferable in view of suppressing pressure loss.
  • external shape of the honeycomb-type structure is arbitrary, and can be selected arbitrarily corresponding to a structure of an exhaustion system where a one-piece structure-type carrier is applied, such as a circular column-type with a true circle in cross-section or an ellipse, a tetragonal column-type, a hexagonal column-type.
  • a thickness of the cell wall of such a honeycomb-type structure is preferably 2 to 12 mil (mill inch), and more preferably 4 to 8 mil.
  • Such a honeycomb-type structure includes one whose material is a metal or ceramics.
  • a metal one made of stainless steel is general.
  • ceramics cordierite, mullite, alumina, magnesia, spinel, silicon carbide or the like is included, however, in view of good formability to produce the honeycomb, and superiority in heat resistance or mechanical strength, it is preferable to be made of cordierite.
  • the upper layer of the honeycomb structure-type catalyst (X) as the upstream catalyst contains the Rh component effective in purification of NO x .
  • Rh is used in the upper layer of the honeycomb structure-type catalyst to promote purification of NO x in exhaust gas by small amount of the Rh component. That is, the Rh component is contained in each catalyst composition in an amount of 0.01 to 2 g/L, and desirably 0.05 to 0.5 g/L.
  • the too much amount may excessively increase concentration of the Rh component, by which sintering of the Rh component may proceed excessively after a durability test in some case, and the Rh component, in which sintering proceeds excessively, decreases surface area, decreases activity, and may not provide performance corresponding to amount of the noble metal. On the contrary, the too less amount may not provide activity necessary in some case.
  • This Rh component is loaded on the following support material of the zirconium oxide, however, a part of the Rh component may be loaded on a material other than the following zirconium oxide, within a range not to obstruct an action of the present invention.
  • the Pt component and the Pd component are not substantially contained.
  • the catalyst composition containing, an oxide not containing the cerium component and having zirconium oxide as a main component, and the following cerium-containing oxide, is used.
  • the zirconium oxide loading the above Rh component is contained in an amount of 1 to 300 g/L, and desirably 15 to 150 g/L.
  • the too much amount may increases thickness of the catalyst layer excessively and makes difficult to raise catalyst temperature up to temperature suitable for purification.
  • thickened catalyst layer obstructs gas diffusion to a deep part of the catalyst layer, resulting in not providing sufficient activity.
  • the too less amount increases concentration of the Rh component in the catalyst composition, resulting in proceeding of sintering of the Rh component, in exposure to high temperature in use, reducing active surface area, and may not providing activity comparable to the use amount in some cases.
  • this zirconium oxide can be used as a support material loading the above Rh component, however, it can be used also as a hydrogen generating material or a binder, by adding to the catalyst composition.
  • the cerium-containing oxide in the upper layer is a cerium-containing oxide as the OSC not loading the Rh component.
  • This cerium-containing oxide may be pure cerium oxide, however, it is preferable to be the cerium-zirconium composite oxide.
  • the cerium-zirconium composite oxide is known as the OSC superior in storing and discharging performance of oxygen, along with heat resistance.
  • a rare earth metal element, a typical metal component, a transition metal component, an alkali metal component, an alkaline earth metal component, other than the cerium component and the zirconium component may be contained.
  • This cerium-zirconium composite oxide is not especially limited, however, content of cerium, in an oxide equivalent, is preferably 10 to 70% by weight and more preferably 30 to 60% by weight.
  • the too much amount of the cerium component results in sintering at high temperature and may decrease capability as the OSC. In addition, the too less amount may not exert sufficient capability as the OSC.
  • the cerium-containing oxide not loading the Rh component is contained in an amount of 0.5 to 200 g/L, and desirably 1 to 50 g/L. The too much amount results in increasing thickness of the catalyst layer excessively and makes difficult to raise catalyst temperature up to temperature suitable for purification.
  • the cerium-zirconium composite oxide is used as an oxide containing such a cerium component, it may be referred to hereafter as CeO 2 / ZrO 2 (B).
  • a support material of the following cerium-zirconium composite oxide loading the Rh component (hereafter may also be referred to as CeO 2 ⁇ ZrO 2 (A)) is included.
  • the Rh component is contained in each catalyst composition, in an amount of 0.01 to 2 g/L, and desirably 0.05 to 0.5 g/L.
  • the Pt component and the Pd component are not substantially contained in this upper layer.
  • amount of cerium is 1 to 20% by weight, as converted to an oxide, and amount of zirconium is 99 to 80% by weight, in an oxide equivalent, and preferably amount of cerium is 1 to 10% by weight and amount of zirconium is 99 to 90% by weight.
  • amount of the cerium component and the zirconium component is too many or too less, purification performance of NO x decreases.
  • CeO 2 ⁇ ZrO 2 (A) is contained in an amount of 1 to 300 g/L, and desirably 15 to 150 g/L.
  • the too much amount may increases thickness of the catalyst layer excessively and makes difficult to raise catalyst temperature up to temperature suitable for purification.
  • thickened catalyst layer obstructs gas diffusion to a deep part of the catalyst layer, resulting in not providing sufficient activity.
  • the too less amount increases concentration of the Rh component in the catalyst composition, resulting in proceeding of sintering of the Rh component, in exposure to high temperature in use, reducing active surface area of the Rh component, and may not providing activity comparable to the use amount in some cases.
  • a material having a desired cerium / zirconium ratio may be selected from commercial products, however, it may be produced by dissolving cerium nitrate and zirconium oxynitrate with ion-exchanged water, adjusting pH, if necessary, and then by the steps of filtering, washing, drying, calcination and pulverization. In adjustment of the cerium / zirconium ratio, ratio of cerium nitrate and zirconium oxynitrate may be adjusted as appropriate.
  • a material such as a binder may be used in a range not to suppress an action of the present invention.
  • alumina, zirconia, silica, titania, silica-alumina, carious kinds of zeolites or the like is included.
  • a compound such as nitrate, sulfate, carbonate, acetate of Rh, Pt and Pd is used.
  • chloroplatinic acid (IV), diammineplatinum (II) nitrite, a solution of amine platinate hydroxide, chloroplatinic acid, diammine dinitro palladium, palladium nitrate, palladium chloride, rhodium (III) chloride, rhodium (III) nitrate or the like is included.
  • the noble metal component in order to load the noble metal component onto an inorganic support material such as alumina or a zirconium-type oxide, it may be performed by a known method such as impregnating the above raw material of the noble metal component into a support material, loading by an ion exchanging method, or kneading the support material and the raw material of the noble metal component.
  • the Ba component is preferable and, for example, barium oxide can be used. It may be added into the catalyst composition as barium oxide, however, it may be selected as appropriate from barium acetate, barium sulfate, barium carbonate, barium nitrate, barium sulfite or the like.
  • the raw material of the NO x storing component other than barium oxide is fired in the production step of the honeycomb structure-type catalyst, and finally converted to barium oxide, or a composite material of barium oxide and other barium components.
  • the inorganic support material loading the noble metal catalyst component by the above method is converted to a slurry-like mixture by mixing with other catalyst component and a binder, along with an aqueous medium, and then coated onto the honeycomb-type structure (it may also be referred to as one piece structure-type carrier), dried and fired.
  • the slurry-like mixture differs in kind of the noble metal catalyst component, or presence or absence of the alkaline earth metal, depending on those for catalyst lower layer, upstream catalyst upper layer, and downstream catalyst upper layer, therefore at least three kinds must be prepared.
  • the aqueous medium is used in an amount which is capable of dispersing uniformly the inorganic support material loading the noble metal catalyst component in the slurry.
  • an acid or an alkali may be formulated to adjust pH, if necessary, or a surfactant, a resin for dispersing or the like may be formulated to adjust viscosity or enhance slurry dispersing property.
  • a mixing method for the slurry pulverization mixing by a ball mill or the like is applicable, however, other pulverization or a mixing method may also be applied.
  • the slurry-like mixture is coated onto the one piece structure-type carrier.
  • the coating method is not especially limited, however, a wash coat method is preferable. After the coating, by performing drying and calcination, the honeycomb structure-type catalyst loading the catalyst composition can be obtained.
  • drying temperature is preferably 100 to 300°C, and more desirably 100 to 200°C.
  • calcination temperature is 300 to 1200°C, preferably 400 to 800°C and particularly preferably 400 to 600°C.
  • Heating means may be performed by a known heating means such as an electric furnace, a gas furnace.
  • the above coating, drying, and calcination on the honeycomb-type structure may be repeated every the catalyst composition to form the upper layer and the lower layer, or by performing slurry coating sequentially and finally drying and calcination may be performed.
  • the honeycomb structure-type catalyst to be used in the present invention is composed of the upper layer and the lower layer where the catalyst composition is coated on the honeycomb-type structure, however, a coating layer may be provided separately, if necessary, at still more the lower side of the lower layer, or between the upper layer and the lower layer, or at still more upper side of the upper layer.
  • a coating layer may be provided separately, if necessary, at still more the lower side of the lower layer, or between the upper layer and the lower layer, or at still more upper side of the upper layer.
  • the coating layer to be provided separately there may be provided a base coat layer to make bonding among the catalyst layer, the honeycomb-type structure and the catalyst layer firmly, or a catalyst layer with different composition, in a range not to obstruct an action of the present invention.
  • the Pt component or the Pd component as an oxidative active species, as well as the Rh component as a reductive active species are used, along with the OSC, therefore it is preferable that it is arranged in a flow passage of exhaust gas exhausted from an automotive gasoline engine operated in a state where fuel concentration of mixed air repeats a lean state and a rich state, to form the TWC for purifying HC, CO and NO x .
  • Sulfur content has been decreasing year by year in commercial gasoline, therefore according to the present invention, a cheap and high performance catalyst apparatus can be provided using the Pd component as a major oxidative active species.
  • Rh / [ZrO 2 ] indicates that the Rh component is loaded on ZrO 2 ) of the essential components of the present invention
  • the catalyst composition of the upper layer of the downstream catalyst hereafter may be referred to as Rh / [CeO 2 ⁇ ZrO 2 (A)].
  • Rh / [CeO 2 ⁇ ZrO 2 (A)] indicates that the Rh component is loaded on CeO 2 ⁇ ZrO 2 (A)) of the essential components of the present invention, so that purification of NOx in exhaust gas is promoted.
  • the Rh component has two cases: one where it is present as rhodium oxide, and the other where it is present as metal rhodium not yet oxidized. And, catalytic activity is said higher in metal rhodium than in rhodium oxide.
  • the Rh component and a support material when the support material is the cerium-zirconium composite oxide, the Rh component is loaded on cerium oxide and zirconium oxide.
  • the Rh component on cerium oxide tends to become rhodium oxide by bonding with oxygen discharged from cerium oxide, whereas the Rh component on zirconium oxide is difficult to be oxidized and is considered to be present as metal rhodium in many cases.
  • Zirconium is a transition metal element capable of storing and discharging of oxygen, and an oxide thereof may act as the OSC in some cases, however, ZrO 2 is inferior to CeO 2 in capability as the OSC.
  • ZrO 2 rarely promotes oxidation of the Rh component, because of low capability as the OSC.
  • Rhodium oxide rarely reduces amount of active metal rhodium in the Rh component loaded on ZrO 2 , because of inferior activity to metal rhodium, and thus it is considered that a state of high purification activity of NO x is maintained. It is considered that zirconium oxide promotes purification of NOx by a steam reforming reaction by interaction with the Rh component, and exerts superior purification performance of NOx when it becomes Rh / [ZrO 2 ].
  • Rh / [ZrO 2 ] + CeO 2 ⁇ ZrO 2 (B) where CeO 2 ⁇ ZrO 2 (B) is present in the same composition while having high reducing activity of Rh / [ZrO 2 ], capability as the OSC is also exerted.
  • the OSC also acts adsorption of an oxygen atom of NO x , as well as oxygen storage. By the Rh component and the OSC being present at a near position, oxygen concentration in exhaust gas is adjusted and purification of NOx is promoted by the Rh component.
  • CeO 2 acts as the OSC, and the Rh component has an action to bond with oxygen, because of being an oxidative active species as well.
  • CeO 2 loaded the Rh component (hereafter may be referred to as Rh / [CeO 2 ]) is used as a catalyst at the downstream side, and the Rh component promotes storage of oxygen to cerium oxide.
  • the Rh component promotes discharge of oxygen for Ce 2 O 3 converted to CeO 2 by storage of oxygen.
  • the action to promote storage and discharge of oxygen in this OSC is considered to work also for an oxygen atom of NO x . That is, it prevents exhaustion of NO x by temporal adsorption of NO x unable to purify, onto CeO 2 .
  • CeO 2 stores oxygen in exhaust gas, it has an action to store oxygen at the vicinity of the Rh component and increase concentration of the reducing component.
  • Rh / [CeO 2 ] has fear of decreasing activity by oxidation of the Rh component, it is considered that purification of NOx is promoted also by such an action.
  • Rh / [CeO 2 ⁇ ZrO 2 (A)] in the present catalyst can also be said a state that Rh / [CeO 2 ] and Rh / [ZrO 2 ] are present together. It is considered that purification of NOx is promoted by interaction of adsorption and discharge of NO x by Rh / [CeO 2 ], and reduction of NO x by Rh / [ZrO 2 ] by this state.
  • the cerium-zirconium composite oxide is also a material superior in heat resistance, therefore it is considered that it can suppress degeneration of the Rh component leading to decrease in activity, such as sintering, and stable purification performance of NOx is exerted, even when the Rh component is loaded. It should be noted that, because storage and discharge of oxygen are also performed in CeO 2 ⁇ ZrO 2 (A), it is without saying that also purification of HC or CO is promoted in the lower layer.
  • Rh / [ZrO 2 ] + CeO 2 , Rh / [CeO 2 ⁇ ZrO 2 (A)] are catalysts each having different activity.
  • high purification performance of NO x is exerted by interaction of such activity difference.
  • oxygen concentration of exhaust gas varies largely.
  • the OSC having high capability of storage and discharge of oxygen is used in the catalyst layer having a purification action of NO x , purification of NO x and buffering of variation of oxygen concentration are performed at the same time to reduce concentration of NO x in exhaust gas and adjusted to a concentration region (a window region) of reducing components, where the downstream catalyst exerts high purification activity.
  • exhaust gas combusted in a state, where variation of air / fuel ratio is large cannot be purified sufficiently only by the upstream catalyst, however, in the present invention, by combination with the downstream catalyst, it is purified substantially.
  • lean indicates a state where an engine is operated in a lean combustion state
  • rich indicates a state where an engine is operated in an excess fuel state
  • stoichiometric indicates a state where an engine is operated at the vicinity of a theoretical air/ fuel ratio. "stoichiometric” is said to be a window region in the present invention.
  • the a) in Figure 3 is a lean combustion state (lean), and in the upstream catalyst, oxygen in exhaust gas is stored and NO x is adsorbed by the OSC of the upstream and the cerium-containing component (not shown) of the lower layer.
  • NO x is stored by the alkaline earth metal component contained in the lower layer.
  • the Rh component is loaded also on Ceria (CeO 2 ), and storage of oxygen and adsorption of NO x are promoted via the Rh component.
  • alkali-earth (the alkaline earth metal) component is contained, and NO x is stored.
  • NO x in exhaust gas is purified by adsorption or storage rather than decomposition of NO x .
  • the b) in Figure 3 shows a purification process of exhaust gas exhausted from a combustion state (stoichiometric) in theoretical air / fuel ratio.
  • the Rh component loaded on ZrO 2 purifies NO x to N 2 by the reducing components in exhaust gas at the active metal surface.
  • reduction of NO x is promoted by the reducing components in exhaust gas or a hydrogen atom generated by a steam reforming reaction.
  • the reducing components in exhaust gas generate by incomplete combustion of fuel, and component concentration thereof is low in a lean state.
  • NO x concentration in exhaust gas decreases, NO x stored by the alkali-earth is discharged by chemical equilibrium.
  • NO x discharged purification of NO x is promoted by an action of the reducing components in exhaust gas or the Rh component (the Rh component loaded on ZrO 2 ).
  • variation of oxygen concentration in exhaust gas is buffered, and a state of a window region, where purification of NOx is promoted, (here, stoichiometric) is maintained for a long period, by the OSC in the catalyst composition of the present invention, and thus purification of NO x is promoted.
  • the c) in Figure 3 shows a purification action by mainly Ceria in exhaust gas in a state where fuel is excess (rich).
  • exhaust gas becomes reducing atmosphere.
  • oxygen stored in the OSC is discharged as active oxygen (O*), and oxidizes HC or CO (not shown) by the Pt component and the Pd component.
  • NO x which had adsorbed on the OSC, is discharged and reduced by contacting with the Rh component having active metal surface.
  • active oxygen "O*" discharged is supplied to an oxidation (not shown) of HC or CO in the Pt component and the Pd component.
  • NO x discharged is reduced by contacting with the Rh component having active metal surface, via the Rh component on the Ceria.
  • Such purification of NOx is promoted in a rich state where amount the reducing components is high, and in a stoichiometric state.
  • an important function in the TWC is a purification function of NO x .
  • NO x purification reactions there is a reaction in which hydrogen generated by other reaction reduces NO x adsorbed at active sites.
  • a reaction for generating a hydrogen which occurs in automotive exhaust gas
  • a steam reforming reaction and a water gas shift reaction are known.
  • the water gas shift reaction is one for generating hydrogen according to the following formula (1) by utilizing CO in exhaust gas, and it is promoted at relatively low temperature ( JP-A-2007-196146 , paragraph 0008, or the like) .
  • generation of hydrogen by the water gas shift reaction is promoted in the presence of Pt ( JP-A-2006-68651 , paragraph 0034, or the like).
  • honeycomb structure-type catalyst to be used in Examples and Comparative Examples were produced by a method shown below.
  • the catalyst composition slurry-5 was prepared similarly as in the catalyst composition slurry-2, except that zirconium oxide, [Zro 2 ] , of the catalyst composition slurry-2 was replaced with CeO 2 ⁇ ZrO 2 (A).
  • the catalyst composition slurry-6 was prepared similarly as in the catalyst composition slurry-4, except that CeO 2 ⁇ ZrO 2 (A) of the catalyst composition slurry-4 was replaced with [ZrO 2 ] , and CeO 2 ⁇ ZrO 2 (B) was added to adjust amount of cerium.
  • the catalyst composition slurry-7 was prepared similarly as in the catalyst composition slurry-1, except that barium hydroxide [Ba(OH) 2 ] of the catalyst composition slurry-1 was replaced with ⁇ -alumina as a binder.
  • the catalyst composition slurry-8 was prepared similarly as in the catalyst composition slurry-3, except that barium hydroxide [Ba(OH) 2 ] of the catalyst composition slurry-3 was replaced with ⁇ -alumina as a binder.
  • the catalyst composition slurry obtained in this way was each coated on the following flow-through-type honeycomb carrier as the lower layer or the upper layer, by a wash coat method, and then via drying and calcination, the honeycomb structure-type catalyst was obtained.
  • the apparatus of the catalyst for purifying exhaust gas corresponding to Examples and Comparative Examples were configured.
  • Composition of each catalyst material and amount of the catalyst component are shown in the following Table 1. Numerals shown in a parenthesis in Table 1 is content of the catalyst component per unit volume, in the honeycomb structure-type catalyst.
  • Figure 9 schematic drawings of the honeycomb structure-type catalyst are shown as Figure 4 to Figure 9 .
  • a composition part different from Example 1 is shown by an oblique line.
  • Figure 9 is a configuration where the catalyst composition slurry in Example 1 was replaced for the upstream catalyst and the downstream catalyst.
  • honeycomb structure-type catalysts of Examples and Comparative Examples obtained in this way, purification performance of exhaust gas was evaluated under the following measurement conditions.
  • JC08 mode evaluation was performed by a chassis dynamo, using a commercial vehicle mounted with a gasoline engine of 2.4 L displacement.
  • the JC08 mode is a running mode of a vehicle, and a running mode where acceleration is not constant but changed delicately to both of a plus side and a minus side.
  • 10 ⁇ 15 mode it can be said to have a content nearer to a practical running pattern, and all exhaust gas exhausted from a vehicle to be tested are measured.
  • the test is performed in both of a state that an engine has been warmed in advance (hot start), and a state that an engine is in a completely cold state (cold start) .
  • Amount of discharge of NO x in the cold start is shown in Figure 10
  • amount of discharge of NO x in the hot start is shown in Figure 11
  • amount of discharge of THC (total hydrocarbon) in the cold start is shown in Figure 12
  • amount of THC (total hydrocarbon) in the hot start is shown in Figure 13 .
  • Rh component loaded on a support material ZrO 2 substantially not containing the cerium component, and having zirconium oxide as a main component is maintained in a metal state.
  • Rh / [ZrO 2 ] is superior in performance of the steam reforming reaction from a stoichiometric region to a rich region, while relatively inferior against variation of A/F (air / fuel ratio). Decrease in purification performance of NO x caused by this variation of A/F is compensated by the cerium-containing oxide.
  • the Rh layer of the downstream catalyst is configured by the Rh component loaded on an oxide support material substantially not containing the cerium component, and having zirconium oxide as a main component, A/F variation cannot be absorbed, resulting in decrease in purification performance of NO x . This significantly appears in particular, in the hot start, where concentration of NO x becomes high.
  • Comparative Example 5 it is considered that because catalyst arrangement was exchanged for the upstream side and the downstream side of Example 1, similarly as in Comparative Example 2, it results in that the Rh layer of the downstream catalyst substantially does not contain the cerium component, and is configured by the Rh component loaded on an oxide support material having zirconium oxide as a main component, and also because of absence of Pt in the downstream side, progress of the water gas shift reaction of the downstream catalyst becomes difficult, purification performance of NO x results in decreasing.
  • the apparatus of a catalyst for purifying exhaust gas of the present invention can be used for purification of carbon monoxide (CO), a hydrocarbon (HC), and a nitrogen oxide (NO x ) in exhaust gas exhausted from an internal combustion engine of a gasoline automobile, a diesel automobile or the like.
  • CO carbon monoxide
  • HC hydrocarbon
  • NO x nitrogen oxide

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  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Health & Medical Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Toxicology (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Catalysts (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)
  • Exhaust Gas After Treatment (AREA)
  • Electrical Control Of Air Or Fuel Supplied To Internal-Combustion Engine (AREA)
EP09800263.7A 2008-07-25 2009-04-23 Katalysatorvorrichtung zur abgasreinigung und abgasreinigungsverfahren Not-in-force EP2308592B1 (de)

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JP2008192389A JP5386121B2 (ja) 2008-07-25 2008-07-25 排気ガス浄化触媒装置、並びに排気ガス浄化方法
PCT/JP2009/058050 WO2010010747A1 (ja) 2008-07-25 2009-04-23 排気ガス浄化触媒装置、並びに排気ガス浄化方法

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DE102013210270A1 (de) 2013-06-03 2014-12-04 Umicore Ag & Co. Kg Dreiwegkatalysator
WO2015135983A1 (de) 2014-03-13 2015-09-17 Umicore Ag & Co. Kg Katalysatorsystem für benzinverbrennungsmotoren mit dreiwegekatalysatoren und scr-katalysator
US9486793B2 (en) 2012-06-06 2016-11-08 Umicore Ag & Co. Kg Start-up catalyst for use upstream of a gasoline particulate filter
US9522360B2 (en) 2012-06-06 2016-12-20 Umicore Ag & Co. Kg Three-way-catalyst system
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JP6175275B2 (ja) * 2013-05-16 2017-08-02 株式会社キャタラー 排ガス浄化用触媒
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PL3097977T3 (pl) * 2014-01-22 2022-01-10 Umicore Shokubai Japan Co., Ltd. Katalizator oczyszczania gazów spalinowych dla silnika zasilanego mieszankami ubogimi paliw
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Cited By (10)

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US9486793B2 (en) 2012-06-06 2016-11-08 Umicore Ag & Co. Kg Start-up catalyst for use upstream of a gasoline particulate filter
US9522360B2 (en) 2012-06-06 2016-12-20 Umicore Ag & Co. Kg Three-way-catalyst system
DE102013210270A1 (de) 2013-06-03 2014-12-04 Umicore Ag & Co. Kg Dreiwegkatalysator
WO2014195196A1 (de) 2013-06-03 2014-12-11 Umicore Ag & Co Kg Dreiwegkatalysator
US10071342B2 (en) 2013-06-03 2018-09-11 Umicore Ag & Co. Kg Three-way catalytic converter
WO2015135983A1 (de) 2014-03-13 2015-09-17 Umicore Ag & Co. Kg Katalysatorsystem für benzinverbrennungsmotoren mit dreiwegekatalysatoren und scr-katalysator
DE102014204682A1 (de) 2014-03-13 2015-10-01 Umicore Ag & Co. Kg Katalysatorsystem zur Reduzierung von Schadgasen aus Benzinverbrennungsmotoren
US10022672B2 (en) 2014-03-13 2018-07-17 Umicore Ag & Co. Kg Catalyst system for gasoline combustion engines, having three-way catalysts and SCR catalyst
EP3632537A4 (de) * 2017-05-25 2020-12-23 Cataler Corporation Katalysatorvorrichtung zur abgasreinigung
EP3699410B1 (de) 2019-02-21 2024-01-24 Johnson Matthey Public Limited Company Katalytischer artikel und verwendung davon zur behandlung von abgas

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EP2308592B1 (de) 2013-04-17
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US8491847B2 (en) 2013-07-23
WO2010010747A1 (ja) 2010-01-28
CN102083531B (zh) 2013-06-05
CN102083531A (zh) 2011-06-01
JP5386121B2 (ja) 2014-01-15
EP2308592A4 (de) 2011-08-03

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